Obtaining neutral distillates from petroleum



OBTAINING NEUTRAL DISTILLATES FROM PETROLEUM James P. Hoihn'an, Wilmington, 'DeL, assignor to Sun' Oil Company, Philadelphia, Pa., a corporation of New Jersey Filed Dec. 10, 1956, SE1. No. 627,229 5 Claims. Cl. 208-263) This inventio'n relates to the refining of petroleum, and more particularly to a novel manner of recovering naphthenic acids and obtaining high boiling neutral lubricating oil distillates.

It is known in the art to refine petroleum containing lubricating oil constituents by vaporizing a portion of the petroleum charge and contacting the vapors with a liquid alkaline material, containing free alkali such as caustic soda. A typical manner of operation involves the use of a vacuum distillation tower containing a flash zone in a lower portion thereof, an alkali treating zone in an intermediate portion thereof, and a rectification zonein an upper portion thereof. The petroleum charge, e.g.. reduced naphthenic crude, is introduced at an elevated temperature into the flash zone, which is maintained under high vacuum, e.g. about 25 to 100 mm. of Hg. absolute. The evolved vapors are passed upwardly through the trays constituting the treating section and are countercurrently co'ntacted with a liquid alkaline material which passes downwardly from tray to tray in the treating section, being withdrawn from the lowest tray in the treating section, and a portion thereof returned to the top tray of the treating section.

Naphthenic acid vapors contained in the vaporized oil react with alkali metal hydroxide to produce alkali metal naphthenates which become incorporated in the liquid alkaline material. These naphthenates are recoverable from the alkaline material by known means and constitute a valuable product of the process. Higher boiling hydrocarbon constituents of the vapors passing through the treating zone become condensed therein and are incorporated also in the liquid alkaline treating agent. The treated vapors pass from the treating section to the rectification section, and are rectified in conventional manner to obtain a plurality of lubricating oil distillates of vary ing boiling point and visco'sity.

In such operation, it is extremely difiicult to produce, in addition to naphthenates, good yields of lubricating oil distillates having high boiling range and high viscosity, e.g. Saybolt Universal viscosity at 210 F. of 100 seconds to 200 seconds o'r more. In order to produce good yields of such distillates as condensates in the lower part of the rectification zone, it is necessary to maintain relatively high temperatures in the alkalitreating zone; The use of such high temperatures frequently results in excessive decomposition of organic materials in thetreating zone, suchidecomposition resulting in carbonaceous deposits which tend to plug up the apparatus and otherwise interfere vin'th the operation. 4

For these reasons, it.has been difiicult or impossible heretofore to produce, in a process involving vapor phase alkali treatment, as heavy lubricating oil distillates as are desired in many instances. The present invention provides a novel manner of obtaining, in such processes, heavy lubricating oil distillates having satisfactory prop erties formany' desirable uses, such distillates being obtained without adverse effect on the operation in thel alkali treating section. v

According to the present'invention, petroleum containing lubricating oil constituents is distilled to obtain a first vaporized portion containing naphthenic acids. which is contacted with liquid alkaline material, as in the alkali treating section of a vacuum tower as described previously. The treated vapors are then passed into the rectification section, wherein various lubricating oil condensates are produced. The extent of the distillation iscontrolled in such a manner that excessive temperaturesare avoided in the alkali treating section, the liquid tern-I perature on the lowest tray thereof being within the approximate range from 575 F. to 725* F., and preferablynot higher than 675 F. Consequently the heaviest lubricating oil condensates obtained in the rectification section are relatively low, boiling, and are lower boiling than lubricating oil distillates obtained in further operations as'subsequently described.

The heaviest lubricatingv oil constituents of the petroleum charge are contained in the residue from the distillation in the vacuum alkalitower, and in one embodi ment of the'invention, these constituents are obtained-as distillate in a subsequent distillation of the residue. This distillate is then contacted with hydrogen under condi-- tions subsequently more fully described, to obtain selective hydrogenation of constituents of the distillates which would otherwise cause undesirable properties. The distil-;

lates thus obtained have satisfactory properties for various applications, and are in general superiorto distillates of corresponding boiling range and viscosity which can be obtained in similar yield in a conventional process in-- Volving alkali treatment of petroleum vapors. The process according to the invention provides valuable alkali naphthenates and neutral high boiling distillates in yields which are not obtainable inprior art operation.

In another embodiment of the invention, lubricating oil distillates having satisfactory properties are obtained from theliquid alkaline material which is removed from the alkali treating zone. In typical operation, such oil constitutes a major proportion of the liquid alkaline material, alkali metal naphthenates and excess alkali metalhydroxide being present in the liquid alkaline material in relatively small proportions. It is known in the art .to. separate the alkali metal naphthenates and alkali metal hydroxide from the hydrocarbon constituents of the liquid alkaline material. According to this embodiment of the invention, heavy lubricating oil having satisfactory properties for various uses is obtained from the separated oil by distillation followed by contacting of the distillate obtained with'hydrogen under conditions subsequently specified.

If desired, the residue obtained ironr the vacuum! alkali tower, and the'rafiinate oil obtained by extraction of alkali naphthenates from the liquid alkaline material can be distilled together to obtain a distillate comprising.

constituents distilled from both charge stocks, the distil late subsequently being subjected to contact with hydrogen under the conditions according tothe invention.

The contacting with hydrogen according to the invention is performedat a temperature within the approximate range from 500 F. to 750 R, and preferably within the approximate range from 600 F. to 700 F.

The pressure is within the approximate range from p.s.i.g. to 2000 p.s.i.g., and preferably within the approxi-v mate range from 1000 p.s.i.g. to 1500 p.s.i.g. The con-. tactng with hydrogen is performed in the presence of a hydrogenation catalyst. A preferred manner of contact- Patented July 5, 1960 silica-alumina compositions; etc.

' 21 to tproduce fa rheavyrlubricatingi v 24 Z'Residue' is withdrawn from towrlithrough line 25, Infzone, 2,4, the distillate is contacted" with hydrogen 'in the presence ofahydrogenationcatalyst,'under con V ditions specified' previously. .1 'I'he hydrogenated heavy V r 3f ing involvespassing the hydrocarbon charge stock downwardly through a stationary bed of granular solid hydrogenation catalyst, in the presence of hydrogen. Preferred space rates in such operation are those withinthe approximate ange from 0.1 to .10 volumes of liquid charge per volume of catalyst bed per hour; more preferred space rates are those within the approximate range 'Hydrogenation catalysts, as well known in the 'ar't, are generally suitable for use according to the invention. E

; amples ofsuitablei'c'atalysts are'metals such as copper,

zinc, ruagnesium-, tin,;-vanadma1, tungsten, chromium,: molybdenum, manganese cobalt, non, nickel, platinum,' .etc'.; or oxides or sulfides of such'metals, or miir'ture's'fof such metals, their oxides of sulfides. Any of' the {well 7, known 'catalyst carriers can be employed" according to V the inventionsuch as activated carbon, alumina, bauxite,

pumice, silica,

charcoal, clay; 'k-ieselguhr, V magnesia,

The invention will-"be fnrtherjdescribed with reference to'the attached drawing, whichfis-a schematic diagram of one embodiment of; the process according to the infvent'ion; e c

aren -em t is subjected to distillation at atmospheric pressure to obtaindistillates comprising gas oil, and lighter pet'roleufrn"v fractions; In a treating section of tower 11 ilther'vapors -evolvedfrorn'thecrude arecontacted with liquid?alkaline njaterial introduced through line '12.

' Liquid alkaline material containing alkali "metal naphthenjates and. gasoil constituents I condensed from. the

vapors, iswithdrawnthrough lin e 13; and introduced into ektractionzone 18. The residue'from the distillation is introduced through line 14mm vacuum tower '15. Lubri-.

cating: oil vaporsecontaining naphth'enic acids, which are evolvedrin tower 15, are passed upwardly through the alkali treating section, and contacted with alkali'rnetal 'hydroxide introduced through line 161 j liquid alkaline material, containing alkali metal uaphi thenates formed in the treating sectionand liquid lubri catingoil'condensed therein, is withdrawn through line 17. -A portion of the withdrawn material 'is returned to the" treating section through means not shown.- Another portion is passed through means not shown into tower 11 to serve as the liquid alkaline material in that tower. Another portion of the liquid alkaline material is passed" through line 17' into extraction zone 18 wherein it is contacted with aqueous isopropanol, introduced by means not" shown, in order to extract alkali metal naphthenates from the liquid lubricating oil The alkali 'metal naphthenates are Withdrawn through line 1?, and the raffinate oil 'is 'withdrawn through line 2-0 and in troduced into yacu'um distillation tower 21. If desired,

a portion of the ralfinate can be recycled through means not'shown to the treating sectionof the vacuumalkali" tower) {Preferably} however, substantially. all of the Lra-flinate is introduced into tower 21f. The'residue. from a vacuunralkali tower 15 islwithdrawn thi'onghline z l and tro'duced into towerf21. The residue an is introduced through line 23 min hydrogenation gone oil which is 'obtained'in zone 24 is withdrawn through line 26, and can, desired,jbef, rcmoved through line 27 e as 'a' product of the process] i'O'n the, other hand, if {further fractionation of the product is desired in order; to ob mm more narrow boiling products," the hydrogenated p'roductc'an be introduced into a distillation zone wherein j such narrow boiling products are obtained. This. distilla tion zone can be a separate distillation zone notshown';

As repre'sentedin thedrawing, crude petroleum is in troduced through line 'int'o atmospheric topping tower f l linate are oil ,distillate which alternatively, the hydrogenated product can be introduced through line 28 into the rectification zone of tower 15, the narrow boiling products being obtained as side streams in the rectification zone. The distillate oils obtained from i 6 the alkali-treated vapors and from the hydrogenated oil are indicated generally by line 30, which represents a pluralityof distillates of difierent boiling range.

If desired, a plurality of distillates' of varying boiling range and viscosity can, be obtained in distillation tower is 21, and one or more of the distillates subjected tohydrogenation as indicated in zone 24. Alternatively, a single hydrogenation zone can be employed, any division of the heavy lubricating 'oil into difierent hydrogenated'di ti'llates being performed subsequent to the hydrogena-' The Saybolt -Universal 'viscosityi at 2 1.0 of the hy- 'drogenatedproductpbtained according t9, the invention is within the approximate range from 100 to 200 sec .20120to150seconds. (7 V we,

The following: examples illustratethe invention:

Examp le l V A procedure generally similaritoithat illustrated the drawing was carried out. Naphthenic crude petroleum havingABl. gravity of about was distilled in theat mospheric' alkali tower to obtaina residue (about 20 ARI.) constituting to of the crude. This'res'idu'e 'cons'tituting"'about 9.5%. based on original crude. The,

. feed inlet temperature for the. vacuum towerwas 6507 F.,-

and the flash zone'pressure mm. of Hg absolute The liquid temperature on. the lowest'trayof the treating; ,1

section was about 630-F. The liquid temperature on the 7 lowest tray above the treating section'was about 600 F.,{

v and the condensate thereon, having Saybolt Universal I removed at a temperature of about '5 F. By stripping ofi about 15 to 20% oflight ends, the viscosity cadbe a raised toabout 135 S.U.S. The next heaviest distillate removed had viscosity of about 78 S.U.S. at 210 F. and

45,was removed at a temperature of about 555 F. By

stripping ofi about 5 to 15% of light ends, the viscosity can be raised to about 85 S.U.S. The residue from the vacuum alkali tower had A.P.I. gravity of about 12,;and

210 F. viscosity of about 1000 S.U.S.

50 Typical yields of distillates obtained in the vacuum 7 alkali tower are as followsz viscosityof 135 S.U.S./210

' F., 2.6.v'olume percent; viscosity of 85 S.'U.S./210 F.,

percent.

ends, and preferably within the approximate range from i.

was distilled in the vacuum-alkali tower tor'obtaina residue 7 viscosity at .210. F. I. of about 135'lsecond's; was; passed.- downwardly into the treating section, The heaviest dis? tilla'te removed fromthe tower had'viscosity of7115 to S.U.S. (SayboltUniversal seconds) at 210 F. and was 9.1 volume percent; and lower viscositiesp 23.0 volume contact,ith'e mixture was Stratified and the alcohollayer 70 due. In cases where alkaline. material from the. atnios phen'c tower is included in the charge to alcohol 'entracai tion, the ratfinate typically has Saybolt Universal yis; cosity at 210 F. .of about 120 seconds. 7 Where alkaline material from the vacuum tower only eharged, the 2.10:? 75 F. viscosity is typically about 280 seconds.

containing naphthenates and alkalimetal: hydroxide was separatedfrom the alkylatelayercontaining oil... Alkylate 1 was stripped from the oil to obtain a rafiinate oil vras resi-i 1 6 A series of vacuum distillations were made, to which were charged blends of vacuum alkali tower bottoms and oil Hydrogenated at Iaifinate oil from naphthenate extraction. These distil- 01m! lations were carried out in a vacuum flash tower from i which a light and a heavy distillate were recovered. Ni- 5 32 f g 5% trogen was added in the preheater coil to assist vaporization. The following table gives the data for the four dis- A.P.I. vit 17 18.3 18.8 hllations: sus at ii m i .5 106.2 107. 1 NPA Oolor Too Dark- 5 4% 3% AgedNPAOolor Too Dark. Too Dark. 7 Distillation Runs 10 Acid No 0.87 0.07 0.03 0 3.1 1.5228..." 1.5213..." 1.5202 1. 5192 No.1 No.2 No.3 No.4 V Distillation F.: 7 Charge inletteinperature,F 723 750 13s 725 E 299' $33 Flash zone pressure, mm. of Hg Abs 41 54 38 15 100 765 3 Llght Distillate: e e e 0 42 "8 2 Vapor temperature, F 575 4.80 530 575 00 912 924 Yield in vol. percent of charge-.- 17. 7 19.7 23. 6 18. 6 0 965 970 A.P.I. gravity oi distillate; 18.3 19.4 19.4 18.3 00 986 ViIscosityof distillate, SKIS/210 66 7 V 50 6 49 2 68 2 0 1,002 1,000 Heavy signing; I 1

%i qiididtemperature,F 635 663 637 638 20 it..:tiss nttaeee at at at itt e eeeeeeeee e e tee eee hydrogenated weee vli cosity o distiiiato, sue 210 5 43 tamed after stripping off small amounts (1.3 to 2%) of Residue, 1 1 1 light ends formed in the hydrogenation. The aged NPA Ziggy; pg g g c r color was obtained after the oil stood at 220 F. for 16 ,Vischsityoir esidue, srs iii'ii' hours In an atmosphere of v p 159-5 219-4 136-2 This example shows that distillate oils having good 7 properties can be prepared, in a process involving dissubstantially higher yields of distillate can be obtained. tillation to produce a residue and vapors and refining of when a stripping um, t a is du e dithe Vapors with liquid alkaline material, by distilling Iectly into the vacuum tower. Thus, for example, about the residue and oil recovered from the liquid alkaline 45 percent of distillate having v scosity at 210 F. of about t i l, d contacting h di m m i h h d 107 S.U.S., can beobtained, using about 6 pounds of preder h dmge ating conditions. The example further heater steam andabout 3 pounds of stnppmg steam per shows that increasing severity of hydrogenation, as pro barrel of chargevided here by decreasing space rate, results in improved The Charge dls'flllatlofls 1 and 2 Was a blflld 0f oils from the standpoint of color, color stability, acidity, 69 volume percent vacuum alkah tower bottoms and 31 m volume percent rafiinate oil from naphthenate extraction; In -mi f h vacuum lk li to b ut 11 Paphtheflates the Vacuum towel Y Present volume percent based on total crude of 107 S.U.S. at m e extractwn p- The charge to dlstlllatwn 3 210 F. distillate having NPA color of, tfor example, 4 was a blend of 77 percent bottoms and 23 percent rafii: 40 can be obtained Attempts to produce higher yields Bate; naphthenates .both the atmosphelflc alk'ah result in decomposition and deposition difliculties in the l and the vaqmm alkali tower were Present m the alkali section and poorer color in the distillate. By .way g Winch prodltcefi the rafiinate' The f i of contrast, in operation according to the invention, smlatlon 4 was similar to the charge to t higher yields of 107 viscosity distillate having NPA color except that 9 f the raflinate 011 was of 4 can be obtained. The following table provides the charge to dlstlnatlpn by a heavy a comparison of the obtainable yields in volume percent distillate oil from the vacuum alkali tower. on total crude. The light and heavy distillates from the four distillations were blended in the following approximate propore Yield of 107 Hons Operation 513139133, Light distillates: Volume percent No. 1 4.05

0 ti 1 ii N0. 7 4-05 Ag c h i' iiing t g the invention. 17 No. 3 11.5 V 4 This example shows that operation according to the Heavy distillates; invention permits obtaining increased yields of heavy N0 3 distillate oils having satisfactory color andother properties. 4 Generally, similar results can be obtained using either 100 00 vacuum alkali tower bottoms or rafi'inate oil from naphthenate extraction asas sole charge stock to the" distil- The blend had-ARI. gravity of 17.8 and Saybolt Unii a i blenfimg iielsemlati's fa 91mm vers a1 viscosit at F of 107 5 seconds 7 of distillations to obtain the hydrogenation charge stock Th y is of course not an essential feature of the invention.

e blend was passed downwardly through a statione Any of the higher viscosity distillates obtained in any of my of 8 to 14 mesh ihydrogenatlon ceatalyst the distillations could be used as the sole hydrogenation prising 20% molybdenum disulfide on an activated alumichar e Stock na carrier, and was contacted with hydrogen during g Exam H such passage under the conditions indicated in the folp lowing table, LHSV representing the liquid hourly space Additional experiments were carried out according to velocity in volumes of charge per volume of catalyst the procedure of Example I, the dist llation of vacuum bed per hour. No hydrogen was removed from the bed alkali tower bottoms and ralfinate 011 being conducted other than that dissolved in the effluent oil, and hydrohowever under somewhat diiferent conditions and the gen was added in amount sufficient to replace that reydrogenation charge stock being a higher boiling trac acted with and dissolved in the oil. tion than that in Example I. e

r The distillation charge stock was a blend of 69 volume ,percent vacuum soda tower bottoms and 31 vol- I ume-percent raflinat'e oil from naphthenate extraction; naphthenates fror'hboth the atmospheric soda tower and Kthervacuum-noda tower were present in the extraction I step-V: fi JfolloWinalahle givesthezdatatoruthe distilla-r o a V a Ch inl mns amre F Flash zone pressure, mm. of gabsolu e fiH a H =j.;; 1- "Lia idstenine amtefEar-11+" -w" 1, Yieldrin vol. percent of charge 131i A.P'.I. gravity; 1"6i9' Viscosity, SU ;ll5,7.0

l Viscosity, s ts/aidin 161.0 The heavy distillate was employed as the-charge to the hydrogen contactingope ation,"whi hwas conducted generally similarlyztozthat in Exampled, th conditions bein .675 13.00 psig, QandMLHsV ;,1.3. The mm. are given;in;the zfQllQwingitahlcr '7 By stripping about 3 of t-lighttends from the product, the viscosity was raised ,from 119.7 to 136.5.

'I hisrexample'shows that heavy distillateshaving good properties can beobtained in a manner generally similar to thatrinvolvred (in Example I, but producing ,a product having higher viscosity than that obtained in Example I; In order .to obtain, in operation oft-the vacuum alkali tower, a 136.5 flviscosity distillate .in :yields correspond ing to that obtained'in example, the temperaturetin the alk alittreating section would have to be raised to ailevel causing severe decomposition and carbon deposition difficulties.

The following table shows the yields of good quality heavy oil obtainable according to'theinventiom as compared; with conventional operation; yieldsare :given in volume percentybase'd on total crude: V n V 8 in Example I are "vacuum distilled in the absence of raflinate oil from naphthenate extraction. The charge stock is a blend of 75 percent iofr the bottoms andZS percent of gas oil :obtained as distillate in the -vacuum' alkalitower. The charge stock iispreheat'ed' to 750? 1 and introduced into a flash :Zone at 64 ot :H absQ lute. iheavy distillate vhaving 210* viscsity f of 7 179 S.U.S.-is obtained, the yield being about 20 voliim'e 3 7 percent -o f-the -distillation charge. This distillate riS charged toawhydrogenationoperation conducted similarly V to that in-Example l, theconditions' being 700 F., 1500' a p.s .i,.g., andLHSV 3; ,f-Ihe product obtained, after stripi ping-of light-ends has approximately the same viscosity 7 as the heavy distillate prior to hydrogenation, zhasvgood color and jcolo'r stability, and'is neutralu .conven' tional operation it is impossible to obtain such :a zhigh vis ccosity distillateuwithout severe operating difliculties be-o cause of the {high temperatures involved.

This example shows that operation according to the invention permits obtaininghigher viscosityrdistillates than are obtainable vin conventional vapor phase alkali treating processes. 7 a 7 1 7 The invention claimed is: e

1; Process for refining petroleum which comprises distilling petroleumcont n ng naphthenic acids and lubricatingoil constituents tooobtain a vaporized portion containing naphthenic acids and woman a residue; contacting said vaporiz d porti n ound r vapor; phase treating co i ion wi tliqn d a l in matetial in a treating zon ther by t f rm alka i metal :naphthena an to cond n r' la ive v hig zboilin hyd ocarbon con ti uents of said P rtion; r m v n treated vapo s iron; the tre i zone; r moving sai igh boiling hyd oc r on ,consti n cuts from said liquid alkaline material; distil ing the bsence .oft qui alk line ma erial a ch rge stockrselected from the group consisting of (1) said residue,

:(Zls i gh boil ng hydro/can onconstituent and mixtures ;of said residue -;and.-saidhigh boiling ihydrocarbon constituents, thereby ,to obtain adistillatethav ing 1Saybolt Universal viscosity at 210 F. ,within :the approximate range from 100 to 200 seconds; contacting the last-named distillate with hydrogen at 5O0 t0f750 V F. and 100 to 2000-p.s.i.g. in-the presence of -a hydrogenation catalyst'to obtaina hydrogenated distillate; and

blending said hydrogenated distillate-and said treated vapors to obtain-distillates containing constituents of both.

=Operation 'l V i i vielaonaas.

V Y -SUSoiL N'PAi Convention 9.] 2% I According.to theinventlonnn; a a 6 :This example shows the? yields ot -good .iguality oil ,having Saybolt;,Universal-!viscosity at 2 l0 =F, of l 36,5 seconds, obtainable-according;to',theinvention. e

Example 'III v r 7 s or V 6.5 V 'Vacuum alkali vtower vbot omspnnd11.cedasdescribe 2. Process according to claim l whereinisaid'blend' ing is performed by dmizdng .said hy o enat ld distillate and said treated vapors and distillingthe resulting ture to obtain said distillates.

V 'Process according to claim 1 wherein said charge stock is-said-residue. e

'4. Process according to claim 1 wherein'said charge stock is said high "boiling hydrocarbon constituents.

'5. Process according to claim"1"whe'rein said charge stock is a mixture of said residue and sa'id high boiling hydrocarbon constituents,

References Cited in the tile or this patent iHQneyoutt June 171, 1257' ings-1 

1. PROCESS FOR REFINING PETROLEUM WHICH COMPRISES: DISTILLING PETROLEUM CONTAINING NAPHTHENIC ACIDS AND LUBRICATING OIL CONSTITUENTS TO OBTAIN A VAPORIZED PORTION CONTAINING NAPHTHENIX ACIDS AND TO OBTAIN A RESIDUE, CONTACTING SAID VAPORIZED PORTION UNDER VAPOR PHASE TREATING CONDITIONS WITH LIQUID ALKALINE MATERIAL IN A TREATING ZONE, THEREBY TO FORM ALKALI METAL NAPHTHENATES AND TO CONDENSE RELATIVELY HIGH BOILING HYDROCARBON CONSTITUENTS OF SAID PORTION, REMOVING TREATED VAPORS FROM THE TREATING ZONE, REMOVING SAID HIGH BOILING HYDROCARBON CONSTITUENTS FROM SAID LIQUID ALKALINE MATERIAL A CHARGE STOCK SEABSENCE OF LIQUID ALKALINE MATERIAL A CHARGE STOCK SELECTED FROM THE GROUP CONSISTING OF (1) SAID RESIDUE, (2) SAID HIGH BOILING HYDROCARBON CONSTITUENTS, AND (3) MIXTURES OF SAID RESIDUE AND SAID HIGH BOILING HYDROCARBON CONSTITUENTS, THEREBY TO OBTAIN A DISTILLATE HAVING SAYBOLT UNIVERSAL VISCOSITY AT 210*F. WITHIN THE APPROXIMATE RANGE FROM 100 TO 200 SECONDS, CONTACTING THE LAST-NAMES DISTILLATE WITH HYDROGEN AT 500 TO 750* F. AND 100 TO 2000 P.S.I.G. IN THE PRESENCE OF A HYDROGENATION CATALYST TO OBTAIN A HYDROGENATED DISTILLATE, AND BLENDING SAID HYDROGENATED DISTILLATE AND SAID TREATED VAPORS TO OBTAIN DISTILLATES CONTAINING CONSTITUENTS OF BOTH. 